Fractionation of hydrocarbon oils



Feb, 28, 19 33. R. w soN 1,899,918

FRACTIONATION OF HYDROCARBON OILS Original Filed Oct. 18, 1926 3 Sheets-Sheet l Feb, 28, 1933. R. E; WILSON FRACTIONATION OF HYDROCARBON OILS 3 Sheets-Sheet 2 Feb. 28, 1933 R. E. WILSON FRACTIONATION OF HYDROCARBON OILS 3 Sheets-Sheet 5 Original Filed Oct. 18. 1926 Patented Feb. 28, 1933 UNITED STATES PATENT OFFICE ROBERT E. WILSON, OF CHICAGO, ILLINOIS, ASSIGNOR TO' STANDARD OIL COMPANY, OF CHICAGO,-ILLINOIS, A CORPORATION OF INDIANA FRACTIONATION HYDROCAlR-BON OILS Original application filed October 18, 1926, Serial No. 142,316. Divided and this application filed October 14, 1929.

'ments .in the fractionation of hydrocarbon oils and refers more particularly to a process and apparatus, 'for such fractionation, which is particularly adapted to be employed with processes for the conversion of higher boiling point hydrocarbon oils into lower boiling point hydrocarbon oils, particularly of the gasoline type, wherein conversion is effected by heating under pressure.

This application constitutes a division of my co-pending application Serial No. 142.316, filed October 18, 1926.

The invention will be fully understood from the following description, illustrated by the accompanying drawings, in which:

Figure 1 is a diagrammatic view partly in section, of apparatus employed for the conversion of hydrocarbon oils, the device of the present invention forming a part thereof; I

Fig. 2 is a vertical sectional view through the fractionating tower of the present invention taken on line 2 of Fig.3;

Fig. 3 is a transverse sectional view taken on line 3 of Fig. 2;

Fig. 4- is a transverse sectional view taken on line 4 of Fig. 2;

Fig. 5 is a transverse sectional View taken on line 5 of Fig. 2;

Fig. 6 is a vertical sectional view of a receiving chamber or drum which receives condensates selected from various points in the fra'ctionating column of Fig. 2; and

Fig. 7 is a vertical sectional view through a vapor fractionating and stripping tower.

Referring more particularly to the drawings, the numeral indicates a furnace setting in which is mounted a pipe coil 21 through which the oil to be converted is passed under suitable condition of pressure and temperature, as hereinafter more fully set forth, to bring it to the desired conversion condition. I

Pipe coils 21 in the setting 20 receive the stock fed them from pipe 22 through the inlet pipe 23, and after it is brought to the desired temperature conditions, and. the latter has been maintained for a suitable length of time, the heated oil is discharged from the Serial No. 399,809.

pipe still through the outlet pipe 24. If desired, more or less of the cooler feed stock may be supplied from the pipe 22 through the valved pipe 25 to the heated oil in the outlet pipe 24 immediately upon its discharge from the pipe still. The heated oil then passes through a pressure reducing valve 26 and enters one or more valved nozzles 27,'or nozzle valves as in my co-pending application Serial No. 112,024, filed May 27, 1926, by which-it is introduced into the enlarged chamber or still 28. preferably tangentially in the lower portion thereof. This chamber is suitably con-, structed of heavy walled material to stand high pressures, although the pressures prevailing therein are not ordinarily as high as those maintained in the pipe coils 21, and is preferably lagged. The enlarged chamber 28 is ordinarily unheated, the temperature attained by the oil in the coils 21 being such that a conversion temperature at which a rapid rate of conversion is attained, is maintained in the chamber 28. The nozzles 27 by means of which the heated oil is introduced into the chamber 28 are preferably tangentially disposed, and the agitation produced by the tangential introduction of the heated oil in the lower portion of the chamber aids in minimizing any settling of tarry 0r coke sediment in the chamber 28. An approximately constant level of liquid is maintained in the chamber 28, a level indicator 29 operated by a float being provided for its observation. Vapors separating from the liquid-in the chamber 28 pass out through the vapor line 31 and enter, preferably tangentially, the lower portion of a lagged fractionating column 32, of the present invention, shown more in detail in Figs. 2, 3, 4 and 5 inclusive. The unvapori zed liquid or residue from the chamber 28 is drawn out substantially continuously through a pipe 33 and enters the tower 32, likewise tangentially, at a point somewhat higher than the point of entrance of the vapors through line 31. Between the point of entrance of the vapor line 31 and that of the unvaporized liquid line or tar line 33 in the column 32 there are provided a number of suitable fractionating plates 35, adapted to tolerprovided a number of fractionatinfi ate considerable coke without clogging, suitably of doughnut and disk type.

At an intermediate point in the column 32, above the point of entrance of the line33 for unvaporized liquid, there is provided a cutoff or trap-out place 36 provided with a central cylindrical conduit or pipe 37 which permits free passage of vapors upwardly from the lower portion of the column 32. Through this cylindrical vapor pipe 37 the vapors en'- ter a compartment of the tower separated from the upper portion of the tower by a partition 38. A pipe coil 39 is provided in the column around the vapor line 37, and vapors rising through the latter pass downwardly through the annular space surrounding it,

passing around the pipe coils 39. Uncondensed vapors enter the external vapor pipes 40 by which they are led back into the column 32 at a point just above the partition 38. i The vapors then rise through a plurality of fractionating plates 41, of which the lowermost is indicated as 41*. Reflux condensate formed in this part of the tower flows downwardly to the lowermost plate 41". This plate, in the form illustrated, is provided with overflow pipes 42, which' discharge into the small collecting chambers 43 connected by pipe 44. From one of these chambers 43, the condensate may be withdrawn through the line 45.

The condensate formed in the compartment between the plate 36 of the column and the partition 38 collects in the annular chamber surrounding the vapor pipe 37 and is withdrawn through the overflow pipe 46 and conduit 47. Below the plate 36 and above the point of entrance of the line 33 there are plates 48, suitably of the bubble-cap type. etween two of these plates, means such as the conduit 49 are provided for the supply of a suitable oil to the column, as hereinafter more fully described. This oil may be, for example, a reduced crude oil.

In order to aid condensation and reflux formation in the upper part of the colunm 32, a suitable hydrocarbon oil, for example, of the kerosene range of boiling points, may be introduced above. the plates 41, for example, through the conduit 50. Vapors uncondensed in the upper portion of the column 32 pass out through the vapor line 51. The column 32 is preferably operated at slightly above atmospheric pressure or at any suitable pressure below the pressure prevailing in the chamber 28, the lines 31 and 33 leading from the latter are suitably provided with suitable pressure reducing valves 52 and 53 respectively.

The oil removed from the column 32 through the line 45 enters the upper-compartment of a two-compartment drum 54. The compartments are formed in this chamber by a partition 55 provided at its lowest point with an outlet pipe 56 leading to the ea ers conduit 57. Both the upper and the lower compartments of the chamber 54 are provided with level indicators 58 operated by floats 59. Liquid oilwithdrawn from the column 32 through the line 47 enters the lower compartment of the drum 54, which is provided with a valved outlet pipe 60 at an intermediate point, this pipe connecting with a valved line 64 leads to a pump 65. From the point where the connection 62 joins the line 57, a valved suction line 66 leads to the pump 67. The pumps and 67 discharge through valved lines 68 and 69 respectively into the line 22 leading to the pipe still 21. Each. of the pumps is likewise provided with a valved discharge connection 70 so that, if desired, the oil discharged by either pump may be forced to storage. By the connections just described,

the pumps 65 and 67 can be made to handle separately the oil from the lower and upper compartments respective of the drum 54; or either pump can be.made to handle the combined oil from both compartments of the drum 54 or any desired proportions thereof. Pumps 65 and 67 are positioned below drum 54.

The vapors pass out of the column 32 through the vapor line 51, to colunm 71, illustrated in section in Fig. 7. The unvaporized liquid or tar from the bottom of the column 32 is discharged through the line 72 and passes through the heat exchanger 73, in which there is a heat exchange between the tar and oil supplied through pipe 125, as hereinafter set forth. The tar is then discharged from the heat exchanger through the pipe 76 to a suitable tar cooler 77, from which it passes out through line 7 8 to a tar pump 79, which discharges from the system through the line 80.

As 'hereinbefore stated, the vapors from the column 32 enter the fractional condensing column 71 at an intermediate point. Above 7 the point of entrance of these vapors, there are provided a number of suitable fractionating plates, for example, bubble plates 81 and below the point of entrance of the vapors, there are likewise provided a plurality umn descends to'the lower portion thereof and preferably a body of such condensate is maintained therein, suitable means, such as the fioat operated indicator 84 being provided for observing its level. If desired, steam may be supplied in the lower portion of the. column 71, preferably below the surface of the condensate collected therein, for example, through the steam line 85 terminating in the perforated coil 86 in the lower portion of the column. The stripped condensate from the column is discharged through the valved line 87 and flows into a receiver 88, from which it is discharged by means of a pump 89. The discharge line 90 of the pump 89 is provided with a valved connection '91 leading to storage and with a second valved connection 92 connecting with the line 50 leading into the upper portion of the column 32, as already set forth.

It is obvious that by means of these connections, controlled proportions of the condensate collected in the receiver 88 may be returned to the upper portion of the column 32 and employed as a cooling medium therein.

Uncondensed vapors passing out of the column 71 through the vapor line 93 enter the condenser 94 and the condensate and cooled gas pass therefrom through line 95 to a separator 96 of any suitable construction. Within the separator 96 separation of liquid and gas takes place, entrained liquid being separated from the gas aided by cold water or other suitable liquid supplied in the upper portion of the separator through the valve-controlled line 98. The separated gas passes out through the line 99 provided with a control valve 100. The condensate, together with the water added pass out from the bottom of the separator 96 through the line 101, which extends to the bottom of a trap 102. The condensate and water pass out of the trap through the line 103 into a separator 104. The pipe 103 enters the separator 104, bending downwardly and opening at an intermediate point therein. \Vater separates from the condensate in the separator 104, and is withdrawn through the outlet pipe 105 which extends downwardly within the separator to the lower portion thereof.

The separated light 'oil condensate overflows throughthe line 106 to the look box 107, from which discharge line 108 leads to the receiver 109. The separator 104,1ookibox 10.7 and receiver 109 are provided with gas vents 110, 111 and 112 respectively, which connect with a manifold 113 leading into a vent pipe 114 from the line 103 to an intermediate point in the gas separator 96.

The light condensate in the receiver 109 passes out through the line 115 to the pump 116, the discharge line 117 which is provided with a valve connection 118 leading to-storage. A second valve connection 119 is provided from the discharge line 117 and leading into the pipe 83 by which this condensate may be supplied to the upper portion of the column 71, as already described. 1

Oil is supplied for use in the system through the line 120 leading to the pump 121, by which it is forced through line 122, entering the coils 39, in which it is preheated by the vapors in the column 32. The oil leaving the coils 39 passes out through the pipe 123 to a vapor separator 124. From age is supplied by line 120 to pump 121, by

which it is forced through line 122 into and through the coils 39, in which it is heated to a temperature which is substantially below that at which appreciable cracking takes place (say, 350 to 450 by the vapors from the'lower portion of the tower 32, the nature of said vapors being more fully hereinafter pointed out. The partially heated oil passes out of the coils 39 through the pipe 123 into the vapor separator 124. As at the I temperature of exit from the coil 39,a substantial amount of vaporization takes place, vapors formed are released in separator 124 and pass out through line 125 into one of the vapor lines 40 leading into the upper part, of

column 32. The liquid or oil from which the lighter vapors have been released passes out of the separator 124 through the line 125 and enters the heat exchanger 73, passing through the tubes therein, the external surfaces of these being contacted with the residual oil from the base of the tower 32. There is some further heating of the oil in its passage through the tubes of the heat exchanger, and it makes its exit therefrom at a temperature of 450 to 550 F. or thereabout.

I The heated reduced crude oil then passes through the line 49 into the flower compartment of the tower 32 above at least some of the circulating or bubble plates 48 therein. The lower compartment of the tower also receives converted oil products at a high temperature, as hereinafter more fully set forth, so that a substantial portion of the crude oil introduced through the line 49 is vaporized by the heat of the converted oil products; i. c., I

the products derived from the conversion system. The vapors from this oil, together with vapors from the converted products also sup-. plied to the lower compartment of the tower, pass upwardly through the conduit 37in the partition 36, the temperature of these vapors being suitably in the neighborhood of 600 to 700 F. and preferably about 650 1B. These vapors, after leaving the conduit 37, pass downwardly through the annular space surrounding it, and in doing so contact with the outer surfaces of the coils 39, through which, as hereinbefore set forth, the crude oil is caused to pass. In the preferred form of construction, as illustrated, the vapors travel in countercurrent to the general direction of movement of the crude oil passing through the coils 39. The vapors then pass out through the vapor lines to the upper portion of the tower. The operation .of the tower will be more fully described hereinafter. The condensate from the vapors formed by the cooling action of the oil passing through the coils 39 collects in the tower on the partition 36 and is drawn off through the line 47 to the lower compartment of drum 54 in which a body thereof is maintained, its level being indicated by the indicator 58 controlled by float 59. A lighter reflux condensate is drawn off from the tower 32 through the line and this flows into the upper compartment of the drum 54, in which a. body of this lighter condensate stock is maintained, its level being observed by means of the float indicator 58. The stock maybe drawn 0E from the-lower compartment of the container 54 through the pipe 61 or through the pipes and 57. The lighter reflux condensate stock collected in the upper compartment of the drum 54 may be drawn ofi through the pipes 56 and 57. The stocks collected in the compartments of drum 54 are each substantially at its boiling point and either stock may consequently be handled at a maximum temperature and with a minimum loss of heat. By suitable connections, which have already been fully described, the oil from either compartment of the drum 54, or mixtures thereof, in any desired proportions may be picked up by-either or both of the pumps 65 and 67 and forced through the lines 68 and 69 respectively into the feed line 22 by which the oil to be converted is fed to the conversion furnace 20. These pumps put the oil under high pressure, suitably a pressure of 900 to 1200 lbs, although if desired pressures from 500 lbs. upwards may be em ployed.

The feedstock, under pressure, is forced through the pipe coils 21 in the furnace 20 in which it is brought to conversion temperature and preferably under such conditions that a very substantial conversion is effected (say from 10 to 25% and preferably above 13%) into desired low boiling point products in the gasoline boiling pointrange at the time the oil emerges from the coil through the outlet pipe 24. The velocity of flow is maintained at such a rate that substantially no deposition of coke takes place within the pipe still 21. The oil is discharged therefrom at teeters a suitable temperature in excess of 780 F, and preferably to a temperature of 850 to 950 F, the pressure at the outlet of the coil being suitably 900 to 1100 lbs.

The heated oil then passes through pressure release valve-26 and through the tan= gential discharge nozzles 27 provided with pressure release valves and enters near the bottom of the enlarged chamber 28 which is preferably insulated so that a conversion temperature is maintained therein. The pressure maintained in the chamber 28 is also very high, (above 100 lbs. per square inch), although preferably not above 7 50 lbs. per square inch. For example, apressure of 250 to 7 50 lbs. per square inch or preferably about 500 lbs. may be maintained therein, The temperature of the material in the interior of the chamber 28 is maintained at from 740 to 860 F, for example, about 800 F.

In order to aid in securing the desired temperature in the chamber 28, feed stock may be diverted from the main feed line 21 through the valved line 25 to the outlet pipe 24' from the pipe still 21. A controlled amount of the cooler feed stock may be supplied through this line to the" heated feed stock emerging from the coil. In this way any desired control of the temperature within the chamber 28 below the temperature at the outlet of the pipe coil may be secured.

In the still 28 a separation of vapors from unvaporized oil takes place. The unvaporized oil, drawn off from a point near the surface of the liquid body in the still through the line 33. enters the column 32 after passmg through the discharge valve 53 by which it is.reduced to a substantially lower pressure, preferably only slightlv above atmos-' pheric; for example, 2 to 5 lbs. This unvaporized oil enters the lower compartment of the column 32 at an intermediate point below 7 the fractionating plates 48 and above the fractionating plates 35. As a result of the reduction of pressure, there is a substantial cooling of the material discharged from the outlet pipe 33, and there is also a substantial WaporiZation of the oil. Under the conditions herein described, the products will be discharged from the line 33 at a temperature of 700 to 750 F. The vapors from the still- 28 pass out through the line 31 and enter, the column 32 in the lower portion thereof, below the plates 35 and below the point of entrance of the line 33 carrying products unvaporized in the still 28. A pressure release valve 52 is provided in the vapor line 31, and is so controlled that the vapors from the still 28 enter the column 32 at a pressure equal to or only slightly more than the pressure at which the products passing through the line enter the column. In general the vapors enter the still at a somewhat higher temperature thanthe products issuingfrom the line 33. Boththe lines 31 and 33 may be caused to enter the column 32 tangentially, as

indicated clearly in Fig. 5.

The vapors released from the products unvaporized in the still 28 and discharged through the line 33 rise in the column 32 and pass through the bubble plates 48 in the customary manner. The unvaporized liquid or tar descends the column and, by the action of the fractionating plates 35 is brought into intimate contact with the ascending vapors brought in through theline 31. These vapors strip the lighter constituents of the liquid, and in this action they are assisted by the fact that they are at a somewhat higher temperature than the liquid itself. At the same time, if desired, steam may be introduced into the column through the line 127. The vapors derived from the converted products rise through the lower portion of the column and pass upwardly through the conduit 37. As has already been pointed out, crude or reduced crude oil. or other feed oil,which has been preheated by contact with vapors in the tower 32, is introduced into the lower portion of the column above the lower ofthe fractionating plates 48 by means of the line 49. A substantial portion of this oil is vaporized by the heat of the products derived from the still 28 and the pipe still 21, and these vapors pass upwardly through the conduit 37 with the vapors from the converted products. The combined vapors then pass downwardly through the annular chamber surrounding the conduit 37 and containing the coils 39 through which the crude oil entering the system is passed for preheating. There is a substantial cooling of the vapors by the cooler oil with the result that a condensate is formed which collects in the annular chamber above the partition 36. The approximate temperature at this point may be, under normal conditions of operation, about 500 to 600 F. The temperature is preferably maintained sufficiently high to cause all of the gasoline fractions and most or all of the kerosene fractions to remain in vapor state. The condensate formed is drawn off through the overflow pipe 46 and the line 47 to the drum 54 to form a part of the feed stock for the pipe still. as hereinbefore described, and consists of vaporized and subsequently condensed por-" tions from both the crude oil andthe conversion products from the system. The vapors pass through the vapor pipes 40 to theupper portion of the column above the partition38 and rise through the bubble plates 41 and 41. Suitable cooling means may be employed in this portion of the tower; for example, a condensate fraction of the nature of kerosene may be pumped into the upper portion of the column through the line 50. Substantially all of the oil so introduced is vaporized and passes out through the vapor line 51 with the uncondensed vapors. The condensed products reflux to the lower plate, from" which the overflow pipes 42 lead to the chambers 43 which are interconnected by pipe 44 and from which reflux condensate is drawn off through the line 45 to the upper compartment of the drum 54. This reflux-condensate which contains both unconverted products directly derived from crude oil or reduced crude oil introduced into the lower portion of the tower 32 and converted products derived from the pressure heating system is of lighter character than the condensate drawn off through the line 47 The temperature conditions within'the upper portion of the column are preferably so maintained that substantially no products of the gasoline range boiling point are retained within the condensate formed and drawn off through the pipe 45, these being largely in the gas oil and /or kerosene range of boiling points. The products of the gasoline together with more or less in the kerosene range of the boiling points pass ofi" through the vapor conduit 51 and enter the fractionating and stripping column 71 at an intermediate point. The vapors rise through the fractionating'plates 81 above their point of admission in the column 71. Suitable cooling means should be provided in the upper portion of the column. A suitable cooling oil, for example, of the nature of the final condensate, may be suppliedabove the uppermost plate through the line 83. .Reflux formed in the column a descends to the lower portion thereof, passing portion. of the column, for example, through the line 85; and .the perforated distributing pipe 86. The steam and vapors pass upwardly through the column and aid in stripping the reflux of its lighter ends. As a result of the action of the column 71,- which may be suitably controlled, vapors of the desired low boiling end products such as those, of the gasoline boiling point range, pass out through the ivapor, line 93, together with such steam as maybe used in the column. The heavier boiling point products,-for example, of the kerosene boiling pointrange, or the heavier por-v tion of the'gasolineform the reflux condensate collectedin the bottom of the column and passes out at a controlled rate of discharge through the line 87 to the receiver 88. From the receiver, it may be picked up by pump 89 and discharged through the line 90, which is provided with two valve connections; one, designated by the numeral 91, leading to storage and the other, designated 92, leading to the line 50 so that any predetermined quantity of these hydrocarbons may be supplied to the upperportion of the uppermost compartment of the column 32 in order to produce the desired cooling action therein, as hereinbefore described. The vapors of the low boiling point products, together with steam pass out of the column 71 through the line 93 and enter the condenser 94, passing through the coil therein, the condensed and cooled products discharging through the line 95 into the separator 96. This separator contains plates suitably of the bubble cap type. The condensed and cooled products enter in the lower portion of the drum or separator 96. The condensed portions are separated and discharged through the line 101. Gas passes out, ascending'through the plates and preferably washed by a hydrocarbon fraction, suitably of the gasoline range of boiling points, supplied through the line 98. The washed gases then pass out through the line 99, preferably to a suitable absorption system for removing therefrom their gasoline constituents.

The separated condensate discharged through the line 101 passes through the trap 102 and out through the line.103 to the water separating device 104. Separation of water takes place in this device, and the separated' water is discharged from the lower portion of the tank through the line 105, while the light oil or gasoline passes out through the line 106 and the look box 107 to the receiving chamber 109. The line 103, the separator 104, the look box 107 and the receiver 109 are provided with vents which discharge through the line 114: into the gas separating drum 96, preferably below the uppermost plate therein.

The gasoline condensate collected in the receiver 109 is picked up through the line 115 by the pump 116 and discharged through the line 117. The latter is providedwith a valve connection 118 leading to a storage and with a second valve connection 119 leading to the line 83 by which controlled quantities of the gasoline distillate may be supplied to the upper portion of the column 71 as a cooling medium therein. While I have described in detail the employment of the fractionating tower of the present invention with one type of process, it is to be understood that it mav be employed with other processes which are concerned with the conversion of hydrocarbon oils.

The foregoing detailed description has been given for clearness -of understanding only, and no unnecessary limitations should be understood therefrom, but the appended claims should be construed as broadly as permissible, in view of the prior art. 1 l

1 claim: v

1. In a fractionating column, a vertical shell, means for supplying vaporizedproducts in the lower portion thereof, fractionating plates above the point of supply of said vaporized products, a partition above said fractionating plates, said partition being proaaeaera vided with a vapor opening, a vapor conduit extend ng vertically from said vapor openmg, said conduit providing a passageway between its wall and the shell of the column,

cooling means in the passageway, said coolmg means effecting condensation of a portion of the vapors emerging from the conduit. means for collecting all condensate above said partition and for withdrawing it from the column at the point of collection therein, a transverse partition spaced above the opening of said vapor conduit, means for collecting vapor from below the cooling means in the passage between the conduit and the shell of the still and for conducting such vapor above the last mentioned partition, fraction ating plates above the last mentioned partition and the point of supply of vapor above ,said partition, cooling means in the shell above said last partition, and means for collecting all condensate formed above the last mentioned partition and for withdrawing it from the column at the point of collection therein.

2. lln a 'fractionating column, a vertical shell, means for supplying vaporizedproducts into the lower portion thereof, means for supplying unvaporized products into the lower portion thereof at a point above the point at which said vaporized products are supplied, fractionating plates between the points of supply of said vaporized and unvaporized products, a partition above said fractionating plates and said points of supply, a second partition spaced above said first named partition, means for conducting vapors from below said first named partition to a point substantially above the same, cooling means between said partitions and below the point at which vapors are supplied above saidfirst-named partition for eiiecting condensation of a portion of said vapors, means for removing all condensate formed by the action of said cooling means, fractionating plates above the second named partition, means for supplying the uncondensed portion of the vapors from a point below said cooling means and above saidfirst named partition to in the lower portion of the shell, fractionating means within said shell above the point of supply of vaporized products therein, means within the column above the said fractionating means fordeflecting upwardly directed vapors to cause them to move in a downward path in a portion of said column. cooling means in said downward path for efiecting condensation for a portion of said means for supplying vapors from the upper vapors, means for collecting, at a point above the said fractionating means and below said cooling means, all the condensate formed by the action of said cooling means, means for removing the condensate directly from the collecting means and the column, fractionating means within said shell above the said vapor deflecting and cooling means, and means for separately removing uncondensed vapors and passing them through said lastna'med fractionating means.

4. A fractionating column comprising a vertical shell, means for supplying vapors in the lower portion of the shell, fractionating means within said shell above thepoint of supply of vaporized products therein, means within thecolumn abovesaid fractionating means for deflecting upwardly directed vapors to cause them to move in a means in said "downward path for efl'ecting indirect heat exchange between said vapors and a relatively cool fluid to eflect condensation for a-portion of said vapors, means for collecting, at a point above the fractionating means and below said cooling means, all the condensate formed by the action of said heat exchange means, means for removing the con- .densate directly from the collecting means and the column, fractionating means within said shell above the said vapor deflecting and cooling means, and means for separately removing uncondensed vapors and passing them to said last-named fractionating means.

5. A fractionating column comprising a vertical shell provided throughout its height with three separate compartments formed by a pair of spaced transverse partition wwalls,

means for supplying vaporized products to,

the lowermost compartment, fractionating plates in said lower compartment above the point of supply of said vaporized products,

portion of said lower compartment to a point above the lowermost portion of the intermediate compartment, a cooling element in said intermediate compartment below the point of supply of vapors to said compartment, said cooling element effecting condensation of a portion of the vapors supplied from the lower compartment to said intermediate compartment, means for withdrawing all of the condensate from said intermediate compartment and for passing it directly from the column, means for withdrawing vapor from said intermediate compartment at a point below said cooling element and for passing it to the upper compartment, fractionating plates in said upper compartment above the point of supply of said vapor thereto, and means for withdrawing all the condensate from said upper compartment 'andfor passfrom the column.

;1 ROBERT E. WILSONi ing it directly downward path in a portion of said column, 

